Process and apparatus for treating mineral oils



April 14; 1936. M. R. FENSKE ET AL 2 7 313 PROCESS AND APPARATUS FOR TREATING MINERAL OILS Filed March 13, 1935 6 Sheets-Sheet 1 April 14, 1936. M. R. FENSKE ET AL 2,037,318

PROCESS AND APPARATUS FOR TREATING MINERAL OILS Filed March 13, 1935 .6 Sheets-Sheet 2 6 Sheets-Sheet 3 April 14; 1936- M. R. FENSKE ET AL PROCESS AND APPARATUS FOR TREATING MINERAL OILS Filed March 13, 1935 TING MINERAL OILS April 14, 1936.

M. R. FENSKE ET PROCESS AND APPARATUS FOR TREA 6 Sheets-Sheet 5 Filed, March 13, 1935 April 14, 1936.

PROCESS AND APPARATUS FOR TREATING MINERAL OILS M. R FENSKE ET!" AL Filed March 15, 1935 a Sheets-Sheet e Patented Apr.. 14, 1936 UNITED STATES PROCESS AND APPARATUS FOR TREATING IVIINERAL OILS Merrell lit. Fenske and Wilbert B. McCluer, State College, Pa., assignorsto Pennsylvania Petroleum Research Corporation, a corporation of Pennsylvania Application March 13, 1935, Serial No. 10,932

24 Claims.

This invention pertains generally to a method and apparatus for contacting liquid phases.

The invention pertains more particularly to a method, and apparatus of the foregoing character wherein high efficiencies are obtained by efiec- The flow of the liquid phases during contact will be referred to as being countercurrent. This term, however, in certain specific instances is subjected to a broad interpretation as will ap- 20 pear hereinafter in the description of such instances.

The longitudinally arranged attenuated packing members may or may not be separately enclosed. I

not separately enclosed to form separate paths for the countercurrently flowing liquids, said packing members are. usually .substantially equally distributed laterally of the counterflow, and substantially the same amount of liquid is caused to flpw over each. Thus substantially the same conditions are caused to exist throughout any lateral cross section of the counterflow when the process isin operation. Should the packing 35 members be of different dimensions, the necessary adjustments as to distribution of packing members and/or of liquid flow may be made to accomplish the same results.

When the longitudinally arranged packingmembers are separately enclosed, for instance, by tubes having relatively small cross sections of any desired geometrical shape, the countercurrently flowing liquids are brought into eflicient' contact in a plurality of separate groups of coun: tercurrently flowing streams or, in other words, in'a plurality of separate phase contacting units. In this case each liquid is preferably metered into each unit in a manner so that at least substaztitially the same results are produced by each. uni

The countercurrently flowing streams may comprise solvent and oil in which case the heavier of the two liquids will usually be introduced into the tower at the top thereof and the 55 lighter at the bottom. v

When they are of the same dimensions and are.

The counterflow, however, may be comprised of two or more immiscible or only partially miscible solvents of different densities in which case the oil may be introduced into the tower at a point or points intermediate the counterflow. 5

The counterflow may also comprise oil flowing in one direction and a pluralityof solvents introduced at different points-along the tower flow-' 'ing in the other direction.

The counterflow may also comprise other combinations as well as other liquids, examples of which will hereinafter appear. 4

Ithas been observed that wetting of the longitudinally arranged packing members by one and perhaps in some cases twooi; more phases plays an important part in theeificiency of con-, tact and the prevention of channeling. These longitudinally arranged attenuated packing members appear to act as guiding elements for at least one phase (and possibly) as it flows through the tower keeping said phase distributed laterally of its flow. The attenuations are preferably of sufliciently small cross section to avoid presenting a path of least resistance of any practicable consequence upon (which terms include through) itself.

'Ihewetting feature makes it possible to disperse the wetting phase (or phases) by virtue of its spreading out into films on the surface of the packing member or members. It has been observed that these films in some cases collect in drops at points on the packing and become detached only to recontact the packing and spread out into films again. This kneading action when present assists in bringing the phase particles to the surface for contact purposes.

While the capacity of a tower having longitudinally arranged attenuated packing members may be increased somewhat by increasing the "cross sections of the packing members, to avoid serious channeling due to too large a cross section, thecapacity preferably will be increased and decreased by increasing and decreasing the number of packing members. The periphery of the tower will then be adjusted to conform thereto.

Thus the attentuated packing members may have any other construction or surface configuration suitable for phase contact in the manner described herein including combinations of the foregoing and from the description it can be seen that when a-phase flows over or about an attenuated packing member this may be over or about the exterior surfaces or the interior surfaces of the attentuated packing member or both. 55

- tion, strips of jack chain, etc.

When tubes are not employed the individual longitudinally arranged .packing members may be of any suitable character, for instance, they may comprise rods of any geometrical cross sec- Such members may carry spaced laterally extending protuberancessuch as discs, spheres, frustums of cones, frustums of double cones, rain-drop shapes or any other surface of revolution to increase the surface. The protuberances on each attenuated packing member may overlap the protuberances on adjacent attenuated packing members so that any drops leaving any protuberances will at once contact another protuberance further downstream to reform into a film. This arrangement of the protuberances also causes the liquids to flow in acircuitous course through the tower.

When tubes enclose individual longitudinally arranged packing members, these members may be constructed as set forth in the preceding paragraph or they may be made up of a large number of separate elements such as raschig rings or similar packing. The separate elements may or may I not be connected together since the packing memwall. 1

Special types of packing are as follows:

1. Smallwire forms such as single turn spirals, polyturn spirals, H shapes, 8 shapes, shapes, open rings, ordinary carding teeth, bent carding teeth and similar forms, all having dimensions comparable to carding teeth used in the textile industry. These forms are found to be extraordinarily efficient, affording a high degree of surface area together with a high degree of free space.

2. Adsorbent material such as fullers earth, silica gel, Florida earth, activated charcoal, and other filtering and contact refining agents-which owe their action to what is called adsorption. These materials are preferably sufliciently coarse to aiford sufiicient free space for a practical rate of counterflow.

However, other types of packing may be employed, for instance, the tubes may be filled with jack chain.

The countercurrently flowing liquid phases may be engaged, that is contacted, continuously throughout the length of the counterfiow or they may ,be disengaged, that is caused to assume a layer formation, at one or more points intermediate the ends of the counterflow. This alternate engagement and disengagement of phases combines in one continuous system the advantages of ordinary continuous countercurrent contact and the advantages of batch contact and particularly batch countercurrent contact.

The layer formation also permits the taking of! of side streams.

Any side stream may be further treated, for instance, in continuous countercurrent for stripping purposes.

The contact between solvent and oil may be of the ordinary character wherein the solvent capacity of the solvent does not vary during the contact. However, it is particularly beneficial in this process because of the avoidanceof serious channeling to set up reflux conditions in the tower. This may be accomplished by reducing the solvent capacity of the solvent in the direction of solvent flow, so that a part of that oil which dissolves in the solvent upon entry of the solvent into the tower is later thrown out of solution before the solvent leaves the tower. This precipitated oil will flow in the same direction as the to the precipitate.

ber may acquire its shape by virtue of the tube employed are repeatedly taken into solution and thrown out of solution and eventually a. sharper separation is effected.

A reduction in solventcapacity in the direction of solvent flow may also be employed for fractional precipitation purposes. In this case a solvent-oil solution is flowed through a tower of the character herein described with the direction of solution flow such that the precipitate will flow countercurrently to the solution. The precipitate is thus scrubbed of its more soluble constituents during its fiow through they tower as a separate phase, these constituents going into solution to replace less soluble constituents which are added Because of the ayoidance of serious channeling, unusually efllcient results may be obtained.

Fractional precipitation may be repeated on the same solution as many times as desired, for in stance, by flowing the solution serially through a plurality of towers thus accomplishing fractional precipitation in stages.

If the solvent-oil solution is brought to an un- 1 saturated condition priorto or upon entry into the tower or towers, for instance, by heating the solution or adding more solvent, a solution zone will be set up in. each tower through which the precipitate must pass. This causes a more effective scrubbing of the precipitate.

When a series of towers are employed for fractional precipitation in stages, a part of the precipitate separated from' any .one tower may be flowed countercurrently through another tower further upstream of solution flow along with the precipitate formed in said tower. The more soluble components of the former precipitate will go into solution to replace therein components of lesser solubility which are addedv to the latter precipitate. A part'of the precipitate separated from each tower of a series, except, of course, the very first, may be fed back into the next preceding tower. Thus, all of the materials are more effectively scrubbed.

Reducing the solvent capacity of the solvent in the direction of solvent flow may be efiected either by reducing the temperature of the solvent, by reducing the concentration of-solvent such as by distillation or evaporatiom'or by adding another solvent which is capable of forming with the first solvent a solvent mixture of lower solvent capacity for the oil.

Further features of the invention reside in the construction, arrangement and combination of parts, and in the steps, combinations of steps, and sequences of steps, all of which, together with other features, will become more apparent to persons skilled in the art as the specification proceeds and upon reference to the drawings in which:

Figure 1 is a sectional elevation of a tower illus I trating one form of the invention;

illustrating a modification of the form of the invention illustrated in Figures 3 and 4;

Figure 6 is a sectional elevation (shown broken) illustrating afurther form of the invention;

Figure 7 is anelevation partly in section illustrating a still further form of the invention;

Figure 8 is a sectional elevation (shown broken) illustrating another form of the invention; and

Figure 9 is an elevational view diagrammatically illustrating a manner of coupling a plurality of towers into a single system.

Referring now to Figures 1 and 2 at III is shown a tower comprising a plurality of tubes ll joined at their ends by tube sheets l2 and I3 and surrounded by a plurality of superimposed chambers ll. Tower III also includes segregating chambers l5 and I6 respectively at opposite ends of tubes II as well as feeding chambers H and I8 also respectively at said opposite ends.

Liquid from chamber I1 is fed into the upper ends of tubes Ii by means of metering tubes 20 and from chamber I8 into the lower ends of tubes H by means of metering tubes 2|.

Tubes ll preferably contain suitable phase contacting means illustrated at 28, for instance,

any of the packing materials referred to above. However, when tubes II are of small inner diameter, packing materials may not be required.

Liquid may be introduced into or withdrawn from tubes H at any point intermediate their ends, for instance, by a device 22 which is illustrated as comprising a conduit 23 communicating with tubes ll through a plurality of metering orifices 24.

Chamber I1 is illustrated as being surrounded by a jacket 26 and chamber I8 is illustrated as being surrounded by a jacket 21.

Any suitable means (not shown) may be employed for introducing heat exchange fluid into and withdrawing the same from the various heat exchange chambers. I

Tubes Il may have a cross section of any desired geometrical configuration and within certain limits of any desired area. The cross section of tubes II is preferably limited to an area sufiiciently small to prevent serious channeling after the contacting means, for instance, packing 28 has been arranged therein.

The preferred limiting cross sectional area for tubes II will be not only a function of the'type of packing employed, since the small wire forms referred to above will as a rule permit the use of a larger cross section: without an inordinate falling off of efliciency thanraschig rings or jack chain, but also of the degree of uniformity of distribution of the packing in the tube. Since the tubes ll may have sides which are straight or indented or of other surface configuration, the departure of a tube from a straight or continuous form will have its influence. For this reason a definite limit in cross sectional area which if exceeded in size will no longer dem onstrate the substantial increase in efficiency which we have discovered results from a constriction, of cross sectional area cannot be given, but .may be readily determined, for instance,

by testing the efilciency of single tubes of different sizes when packed with the packing is to be employed.

It may be stated as a general rule that one should proceed with caution after exceeding across sectional area equivalent to that of a circular tube inthe neighborhood of three inches in diameter, although with the proper selection of which packing and a careful distribution in each tube, it is possible that larger cross sectional areas may be employed, while in other cases smaller cross sections may be required.

Therefore, the term relatively small cross sectional area when employed in this specification and in the claims is intended to mean a cross section which when taken in conjunction with the contacting means (if any) therein is sufiiciently small to materially increase the contacting efficiency because of the constriction of its area.

In those cases in which it is desired to cause heat transfer through the tube walls, consideration should be given to the effect of cross-sectional area upon eflicient heat transfer.

We have successfully employed metallic tubes of various relatively small cross-sectional areas, for instance tubes of circular cross-section and of inch, 1 inch, and of 1.75 inches in diameter, and have obtained both efllcient heat transfer and eflicient phase contact, although it appears that circular tubes up to about 4 inches in diameter might be employed successfully for heat transfer purposes.

Tower III is adapted for many different modes of operation. For certain of these modes, it may be greatly simplified in construction as will hereinafter appear.

Certain modes of operation are as follows:

(1) In this mode of operation solvent and oil are contacted by simple countercurrent fiow. The heavier of the two liquids isintroduced into the upper ends of tubes I i through chamber I1 and metering tubes 20, and the lighter of the two liquids is introduced into the lower ends of tubes ll through chamber l8 and metering tubes 2|. Due to a difference in density the two liquids fiow countercurrently to each other. These liquids are efficiently contacted without serious channeling in view 1) of the attenuated packing membersand/or (2) of the small cross sec tional area of tubes. ll.

Two immiscible solutions are formed, the. lighter of which collects in segregating chamber for instance, through a device 22 midway between the ends of tubes I I. All of the liquids will be prevented from serious channeling (3) In this mode of operation the oil is introduced into the tower at one end thereof,-one sol- ,vent is introduced into the tower at the other end thereof, and one or more solvents are introduced at an intermediate point or points. The densities of the solvents are so chosen that they will flow countercurrently to the oil. The oil as it flows through the tower is first contacted by a mixture of all solvents, and progressively by one less solvent as the point of entry of that solvent is passed, and eventually is contacted by the single solvent which enters the tower at the end, opposite that of the entry of said oil. All liquids are intimately contacted without serious channeling.

The solvents may be completely or partly miscible in the proportions in which they are introduced or may be completely immiscible.

(4) In this mode of operation reflux conditions are set up in the tower. As the oil and solvent flow 'countercurrently, the solvent capacity of the although the solvent remains saturated with oil,

the concentration of dissolved oil decreases due to the precipitation of oil from the solvent caused by the reduction in solvent capacity.

The precipitated materials, being of a density comparable to that of the feed oil, flow countercurrently tothe solvent and back into the zone in which the solvent is unsaturated.

The precipitate in its flow countercurrently to the solvent is brought into intimate contact with the solvent. Thus, any components in the precipitate which are relatively more soluble in the solvent than components which are already in solution in the solvent, will go into solution and displace from solution such less soluble components. a

Since these precipitated material flow into the solution zone, further quantities of relatively more soluble components thereof go back into solution. These components are carried back into the precipitation zone by the solvent. I As a result ofthe continuous repetition of this cycle, a much sharper separation of oil components is obtained and the quantity of components-of the same composition finding their way into both the raifinate and extract phases, is substantially reduced.

Among the advantages over other processes is that all liquids are intimately contacted without serious channeling.

The solvent capacity of the solvent may be reduced in the direction of solvent flow (a) by introducing the oil into the tower at a temperature lower than that of the solvent, for instance,

by employing heat exchange chambers 28 and 21; (b) .by reducing the temperature along tubes II in the direction of solvent flow, for instance, by means of heat exchange chambers H; (c) by introducing into the tubes II at one or more points, for-instance, through the devices 22 a second solvent which is capable of forming a mixture with the first solvent of lower solvent capacity for the oil; (at) by reducing the solvent concentration in the direction of solvent flow, for instance, by withdrawing liquid from tubes ll through any device 22, removing solvent and returning the residuum to the tubes ll through another device 22 preferably adjacent the point of withdrawal; and (e) by a combination of any two or more of the foreging, or otherwise.

If the temperature were reduced in the direction of oil flow, precipitation of solvent from the oil phase instead of oil from the solvent phase would result.

so that only the precipitate will flow through the I precipitation zone. The former sub-mode of operation will be referred to as la and the latter as 41). V

In mode lb the oil might be introduced into the tower through any of the devices 22 at the desired point or points.

Whether thefeed oil flows through the p'recipitation zone as inmode la, or whether it flows only through the solution zone as in mode 412, is of particular importance when side streams (to be,

referred to hereinafter) of precipitate are taken off.

(5) In this mode of operation tower II is used for fractional precipitation pin-poses. The solvent with its dissolved oil is caused to flow throuzh tower II) in a direction which is determined by the density of the precipitate. If the density of the precipitate is greater than that of the solution of solvent and oil, said solution is caused to when the solution is introduced into tower II in an unsaturated condition, since in this case a solution zone, as well as a precipitation zone, is set up in the tower.' A saturated solution may be brought to an unsaturated condition by any suite able means, for'instance, by heating or addinfl more solvent.

By running the solution serially through a plurality of towers in each of which precipitation takes place, either with or without the setting 'up of solution zones, fractional precipitation in stages is effected.

A part of theprecipitate separated in any stage may be fed back into a preceding tower, for instance the next preceding, in a manner' so that it will flow countercurrently to the solution therein. 'This will increase the scrubbing effect particularly if a part of the precipitate separated in each stage except, of course, the very first is fed back into the next preceding tower. A

(6) In this mode of'operation all of the liquids pass through the tower in the same direction but one travels at a greater linear rate than the other or others. Because the liquids travel through the tower at different velocities, there is a relative flow between the liquids which may be referred to as being countercurrent although, strictly speaking, it is not. V To accomplish the foregoing the liquids which are to form the phases may be introduced into tower In at the bottom thereof and caused to flow upwardly therethrough.

If the solvent and'oil are mixed to form a solution or are homogeneously mixed-mechanically, this mixture may be metered into tubes ll either through-chamber IE or through chamber If the solvent and oil are in solution, a part of the oil may be caused to precipitate from solution in tubes H by any suitable means to cause the formation of the phases.

If the solvent and oil are not mixed prior to their introduction into tower l0, one may be metered into the tower through chamber I8 and the other through chamber l6. Inthe construction shown, it would be probably more satisfactory chamber l6.

The liquid oi lesser density travels up through tower ID at a faster rate than the other liquid or liquids.

Because of the construction of tubes II, the two phases are contacted without serious channeling.

The two phases may be separated by formation 10 ,into layers which may take place in chamber I5,

particularly if the construction is varied as indicated in dotted lines, by extending the tubes ll into chamber l5 to deliver the phases to chamber 15 at about the level of the interface between the two phases. The phases may be separately withdrawn from chamber 15 at different levels, for instance, by means of the outlets indicated in full and dotted lines.

When the phases flow up through the column,

' chamber I! need not be employed.

On the other hand, the liquids which are to form the phases may be metered into column Ill through chamber il and/or chamber IS in a manner similar to that previously described in connection with chambers l6 and I 8.

- In this case the heavier phase travels down through the column at a greater linear velocity than the lighter phase and is intimately mixed therewith. Layers .of the two phases may be formed in chamber it and separately withdrawn throughsuitable outlets at different levels. The

lower ends of tubes ll may be extended as illustrated in dotted lines to a point approximately at the interface between the two layers.

Considering the foregoing in. connection with mode of operation 1) above, it will be seen that to obtain relative movement between the two phases one phase may move through tower H) in either direction without change in direction of the other phase, or, in fact, might remain stationary as long as the other phase is in motion.

Therefore, mode of operation (6) may be combined with mode of operation (1) or any other mode of operation herein described to cause the one phase to alternate in direction through the tower Ill should this be desired, or a contact analogous to that obtained in batch contacting may be obtained by holding one phase stationary.

While it may be preferred to have a phase that preferentially wets the packing travel faster than the other phase, the opposite might be resorted to.

(7) In this mode of operation, the flow of one phase with respect tothe other phase, is at an angle less than 180 and greater than This mode of operation may be combined with any of the previously described modes of operation.

A tower more suitably adapted to this mode of operation will be described hereinafter.

The desiderata. in the operation of tower to are (1) that the lighter phase leaving any individual contacting unit shall be of the same composition as the lighter phase leaving any other contacting unit. (2) that the same shall apply with respect to the heavier phase and (3) that the two phases shall be homogeneously mixed in sired capacity.

cause the same amount of precipitation in each tube.

However, the individual contacting units may differ without departing from the spirit of the invention. Such difi'erences may be as to construction, such as size, length, contacting means or otherwise.

For instance, the individual contacting units may vary as to construction but may be matched so that each will deliver lighter phase of substantially the same composition, and heavier phase of substantially the same composition when oil is fed at substantially the same rate to each, and solvent (or solvents) is fed at substantially the same rate to each.

On the other hand, the individual contacting units may be of the same and/or of difierent construction but may differ as to capacity. In this case, adjustments of the oil feed and/or of solvent feed may be made to cause the respective phases from any unit to be of substantially the same composition asthe respective phases from any other unit.

The use of metering tubes 20 makes it possible to adjust the feeding rate of the heavier (or heaviest) liquid (either solvent or oil as the case may be) to any contacting unit by employing a metering tube for that unit of the desired capacity. Likewise, the use of metering tubes 2! makes it possible to adjust the rate of feed of the lighter (or lightest) liquid to any contacting unit by employing a metering tube for that unit of the desired capacity.

When a liquid (or liquids) is introduced into the column intermediate the ends thereof as in modes of operation (2) and (3) and possibly (4) (5), (6) and (7), the use of metering tubes 24% makes it possible to adjust the feeding rate of this liquid (or liquids) to any contacting unit by em ploying a metering tube for that unit of the de- Thus, the desired balance may be obtained. The precision of this balance will, of course, depend upon the results desired and, therefore, may be rough or close according to requirements.

Other variations are possible, for instance, if tubes H are of the same-cross section and are matched as to pressure drop, metering tubes 2! may be omitted, together with their supporting structure. Chambers It and I8 would thus become a single chamber into which the lighter (or lightest) liquid may be fed preferably adjacent its top and from which the heavier (or heaviest) solution may bewithdrawn adjacent its bottom. The ascending lighter (or lightest) liquid, due to the uniformity of cross sectional area and pressure drop of tubes II will divide equally between the various tubes H or in other the quantity of packing and/or the amount of liquid entering individual" heavier (and/or heaviest) liquid entering the individual tubes may be adjusted to obtain solutions from each individual contacting unit of the desired composition.

In modes of operation (4) and (5) the amount of precipitate produced in any individual contacting unit may also be regulated with or without other methods of regulation to obtain the desired balance.

It is thought that the two phases may in a sense be considered as a dispersed phase and a continuous phase in that one phase may pass in film and/or drop form through the other, the former being the dispersed phase and the latter the continuous phase. However, since in a homogeneous mechanical mixture both liquids are in a dispersed condition it may be that, at least in some cases, a continuous phase, strictly speaking, does not exist. It is conceivable, however, that in some cases it would be possible by control of the feed to maintain one phase continuous and the other dispersed. In such cases it would be preferred to disperse the phase which preferentially wets the packing, although the opposite may also be resorted to.

.When the phase which preferentially wets the packing is .dispersed this phase is conducted through each tube over and while wetting the packing medium and in being, so conducted is maintained either entirely in film form or with a portion alternately in film and drop form. The latter also ailords emcient contact because of a sort of kneading action caused by the drops recontacting the packing and re-spreading out into films only to be followed by .the formation of more drops. This brings a large proportion oi. the liquid particles to the surface for contact with the other phase.

s The special packing elements comprising small wire forms herein set forth are unusually efllcient in that they aiford a very high degree of surface area together with a very high degree of free space. These special packing elements are, therefore, superior to other packing of this type.

A construction in which the attenuated packing members are not enclosed in tubes is illustrated in Figures 3 and 4 in which tower 30 is shown as comprising a plurality of rods 3| carrying spaced protuberances 32, a shell 33 having a jacket 34, a feeding chamber 35, a segregating chamber 36, and a combined feeding and segregating chamber 31.

Rods 3| may be supported in tower 30 in any suitable manner, for instance, as-illustrated.

Extending downwardly from feeding chamber 35 about each rod 3| is a metering tube39, which is arranged so that the metered liquid will be deposited onto the rod. v

Tubes 39 are of suflicient length to form with their supporting'plate '40 and the upper-end of shell 33 a segregating chamber 36,

The lower end of each ro'd 3| is illustrated as being surrounded by a segregating tube 4| which forms with the rod an annular space for the downward flow of liquid adhering to the rod. The lower end of each tube 4| is provided with a plurality of apertures 42 to permit said liquid to flow into chamber 31.

Each tube 4| is illustrated as extending beyond the upper end of chamber 31. and with its upper end surrounded by a tube 43 in such a manner as to aflord an, annular space 44 between the tubesformeteringpurposes. 1

, The discs 32 on each-rod 3| are illustrated as.

while adhering to rods 3| and discs 32, collects in tubes 4|, drains out through apertures 42 to form a layer in chamber 31, and is withdrawn at 46.

If any drops of this liquid leave any packing member, such drops almost immediately recontact another packing member and return to fllm form.

The lighter liquid enters chamber 31 at 41 and occupies the upper part of chamber 31. This liquid is metered up through the annular spaces 44 and thus is distributed laterally of the tower As the lighter phase flows up through the tower it intimately contacts the heavier phase.

The lighter solution collects in segregating chamber 36 and is withdrawn through outlet 38.

If the lighter phase wets the packing in preference to the heavier, tower 30 might be constructed up-side-down. The lighter liquid would then be metered onto rods 3| by tubes 39 and the heavier liquid would be metered laterally of the tower by annular spaces 44.

Other suitable means may be provided for metering the liquids and/ or for separating the final phases. For instance, tubes 4| and 43 might be eliminated. The separation in chamber 31 would then be by simple layer formation, and the lighter liquid would be distributed laterally of the tower by virtue of its layer. This arrangement might be preferred, for instance, when the continuous phase preferentially wets the attenuated packing members. i

It is, of course, possible to shape the protuberances 32 so as to substantially avoid the formation of drops, for instance, bymaking protuberances 32 frustums of cones withthe small base pointing downstream of the wetting liquid flow or of similar shape, for instance, with the surface between the large and small base concave or convex. A concave surface would assist in directing the non-wetting liquid through a circuitous course without a material increase and possibly a decrease in pressure drop through tower 30. Protuberances 32 might also be shaped as rain-drops and arranged, for instance, with the nose pointing downstream of the wetting liquid flow and with the tail pointing upstream thereof, or vice versa.

'- For the purposes of clearness a limited num- --ber of attenuated packing members has been shown in the drawings with the volume or free space fairly large of least resistance along the inner wall of shell 33, baflles might be attached to this wall to cause such liquid or liquids to flowback toward the attenuated packing members and to become redistributed.

A manner of metering liquid onto rods 3| in- "termediate the ends of tower 30 is illustrated in Figure 5 in which feeding section 53 may be considered as being interposed intermediate the ends r shell as of Figure 3. 1 correspondingparts of shell 33 are identified as 33a, of jacket 34 as Ila, of rods 3| as 3m, and of protuberances 32 as He.

Feeding section 56 comprises a chamber 5I formed by tube sheets 52 and 53 between which extend a plurality of imperforate tubes 54 and a plurality of perforate tubes 55.

' Imperforate tubes 54 are free of any obstructions whereas a rod 3Ia passes down through each perforate tube 55.

Perforations 56 in tubes 55 comprise meteringorifices through which liquid from chamber- 5| may be metered onto rods file. This may be preferred when the liquid fed into the tower at the intermediate point preferentially wets the attenuated packing members.

However, rods 3'Ia may pass through tubes 54 if desired, and orifices 56 may be employed for distributing said liquid from chamber 5| laterally of the tower, for instance, in case said liquid does not preferentially wet the attenuated packing members.

The metering. of the various liquids into tower 36, whether at two or more points or whether onto the attenuated packing members or not, preferably follows as nearly as possible the principles above set forth in the discussion of tower IIl.

While the metering onto the individual packing members of the liquid which preferentially wets the packing may be preferred, it is not an indispensable feature and other constructions may be employed, for instance, in case there should be no clearly defined preferential wetting.

While heat exchange jacket 34 has not been illustrated as being divided into a number of sections, such construction may be adopted.

. Tower 30 may be used for any of the modes of operation heretofore described in connection with the descriptionv of tower I6.

In connection with the description of tower III, it was pointed out that the packing 28 in tubes .Il may be adsorbent material.

The employment of adsorbent material as packing in the solvent treatment of a lubricating oil particularly when such treatment is for the purpose of extracting unsaturated, asphaltic, and/or naphthem'c constituents,-is especially useful since it assists the solvent in segregating these constituentsfrom the other oil components.

Unsaturated, asphaltic and naphthenic constituents of an oil are preferentially adsorbed generally in the order named. In the solvent treatment of oil for the purpose of removing these constituents, such constituents are preferentially dissolved generally in the order named.

tinuously by modifying the construction of the tower.

A tower adapted for either intermittent or continuous renewal of adsorbent material packing is illustrated in Figure 6 wherein tower 66 comprises a contacting section 6I, a liquid feeding chamber 62, an adsorbent material feeding cham ber 63, a light solution segregating chamber 64, a liquid feeding and segregating chamber 65 and an adsorbent material withdrawing means 66.

Section 6| may have a construction similar to the corresponding part of tower Ill.

Metering tubes 68 extend from chamber 62 through chambers 63 and 64 and enter tubes 69 of section 6I.

Adsorbent. material III is fed into tubes 69 from chamber 63 through tubular filters II which are alined with tubes 69. v

' Adsorbent material I is withdrawn from tubes 69 through tubular filters I2 which extend from the lower ends of tubes 69 through chamber 65 and connect with individual units 13 of withdrawing means 66. i

Each unit 13 is illustrated as comprising a casing I4 and a screw I housed therein.

Units 13 as shown extend into a container 16 in which the withdrawn adsorbent material and any seepage of heavier solution collect.

Screws I5 may be operated individually or in unison, for instance, by the means illustrated. at 11 ifdesired.

In operation, the heavier liquid is fed from chamber 62 through metering tubes 68 into tubes The lighter liquid is fed into chamber 65 at I8, forms a layer therein above the layer of heavier solution, passes inwardly through the walls of filters 'I2,'and ascends through tubes 69 wherein it contacts the descending heavier liquid.

The lighter solution thus formed ascends up into filters I I, passes outwardly through the walls of the, filters and collects in chamber 64 from which it is withdrawn at I9.

The heavier solution descends into filters I2,

passes outwardly through the walls of the filters, and forms a layer in the bottom of chamber 65 from which it is withdrawn at 80.

The adsorbent material may be fed into chamber 63 by any suitable means, for instance, the

means illustrated at 8 I. The feeding is preferably in a manner so that the upper ends of filters II are kept covered.

In the form shown, the absorbent material descends by gravity through filters I I, tubes 69, and filters I2, as permitted by the revolution of screws I5 which discharge adsorbent material into container I6.

Since any seepage into container I6 will be of the heavier solution, this seepage may be withdrawn from container I6 as illustrated at 62 and :gmbined with the heavier solution withdrawn at The adsorbent material may be removed from container 16 by any suitable means, for instance, by a screw or at intervals through a man-hole.

Any other suitable construction may be substituted for that shown in Figure 6, for instance,

one which will cause the adsorbent material to ascend through filters I2, tubes 69, and filters I I, so that it may be withdrawn from chamber 63. Theoretically, this may be accomplished by reversing the rotation of screws I5 and supplying the lower ends thereof with the adsorbent material.

Tower 60 is capable of use in any of the modes of operation heretofore described in connection with tower Ill, changes in construction being made when necessary following the principles above set forth.

&

For instance, tower 69 may be used in mode of operation (6). In this case the adsorbent material may be of anydesired mesh. The ordinary percolation filters may be employed for this purpose ifdesired, but not with the same efliciency since in tower I9 serious channeling through the adsorbent material does not take place when elevated pressures are applied to the liquids.

Theadsorbent material may be introduced into the tower in any other way, for instance by forming a slurry of adsorbent material and one of the liquids to be fed into the tower, the slurry being withdrawn with one of the solutions formed depending upon the relative densities of the materials in the tower.

The invention, however, is not limited to this means of simultaneously contacting solvent and adsorbent material with oil since this may be accomplished by other suitable means, for instance, in batch operations or batch countercurrent operations, by methods comparable to those of contact filtration. I

A form of the invention in which disengagement of phases and the formation of layers is efiected intermediate the ends of the tower, is illustrated in Figure 7. Tower 99 is shown as being of a construction somewhat similar to tower I9 except that tubes 9| are in sections-with the I opposite ends 92 and 99 of each tube 9| projecting into a phase disengagement chamber. These chambers intermediate the ends of tower 99 are shown at 94.

provided with caps 95. Caps 95 are arranged in a manner to avoid locking of the liquids against flow.

The heavier layer in any chamber 94 will collect about the ends 92 of tubes 9| and will overflow said ends. The upper edges 99 of ends 92 are preferably arranged in a horizontal plane so that the heavier layer will be metered into tubes 9|, the quantity metered into any tube 9| being determined by the perimeter of the tube. For instance, if the perimeters of ends 96 are the same, the same amount of the heavier layer will be metered into each tube 9|.

What has just been said applies equally to the feeding of the heavier liquid from chamber 99 into the ends 92 of the uppermost tubes 9|.

The heavier liquid may be fed into chamber 99 as illustrated at 99.

The lighter liquid in any chamber 94 will ac-' liquid the lighter of any'ehamber'fl ends 92 or ends 93 (or both) of tubes 9| may be feeding of the lighter liquid from chamber mis illustrated at I94, and means for feeding liquid into or withdrawing liquid from the heavier layer of any chamber 94 is illustrated at I95.

It is, of course, understood that any number of chambers '94 may be employed, that is one or 5 more.

In some instances, it may be desired to feed a liquid directly into tubes 9|, for instance, this maybe desired when such liquid is a precipitating solvent. For this purpose a device 22 as 10 shown in Figures 1, 2 and '7 may be employed'if desired.

At the ends of tower 99 the lighter solution is segregated in chamber 98 by layer formation and withdrawn at I96 and the heavier solution is segregated in chamber |9| by layer formation and withdrawn at I91.

Heat exchange with tubes 9| may be effected by any suitable means, if desired, for instance by means of the heat exchange chambers I99.

Tower 99 may be employed in any of the modes of operation heretofore listed in discussing tower I9.

Tower 99 is particularly adapted to modes of operation (441), (4b), and (5) to obtain various fractions of oil varying as to quality if the solvent is selective as to molecular type or varying as to boiling point if the solvent is selective as to molecular size. I

Under mode (4a) a part of the feed oil would come ofi with a side stream of precipitate, where- 'as, in mode (412) the side stream would be precipitate without feed oil.

Under mode (5) fractional precipitation in stages may be effected in a single tower.

Under mode (1) the various fractions would also vary as to quality or boiling point according to the solvent employed.

Under modes (2) and (3) similar effects would be produced.

Tower 99 might also be employed for mode (6).

It should be noted that a. fraction taken off in a side stream may be of the poorer quality oil or of the better quality oil if the solvent is selective as to molecular type, or the fraction may be of the materials of lower boiling point or of the materialsof higher boiling point if the solvent is selective as to'molecular size. In other words, the side streams may be of the solvent phase, or 59 of the oil phase, or both.

Any of the side streams withdrawn from tower 99 may be retreated with solvent, for instance, for strippingpurposes; -This maytake place in a side tower such as illustrated at I99.

Disengagement of phases between the ends of a tower may be effected by other means, without departing from the spirit of the invention.

A tower in which the flow of one phase with respect to the other phase or phases is at an angle greater than 0 and less than as called for in mode of operation (7) is illustrated in Figure 8.

In this figure, tower I49 has a construction which is very similar to that of tower 99 of Figures3 and 4. The chief diilerences are the elimination of tubes 4| and 49 of Figure 3, the addition of one or more plates I 4| which extend laterally of the tower I49 and divide said tower into 7g a plurality of chambers I42, and the provision of manifolds I49 on opposite sides of chambers I42. Plates I 4| are provided with apertures I44 through which extendrods 9Ia of the attenu ated packing. apertures I44'i'are mt? ficiently large to permit liquid flowing along rods the flow of the vertically moving phase therethrough in preference to the laterally moving phase.

Branches I46 of the manifolds I43 may be provided with adjustable valve members I41 so that the fiow of continuous phase through the individual branches I46 may be regulated.

- The distribution of branches I 46 on opposite sides of tower I40, whether the tower has a circular, square, rectangular or other geometrical cross section, is such that, as the liquid flows out of branches I46 and into a chamber I42 on one side and flows out of said chamber I42 and into branches I46 on the other side, such liquid is effectively distributed about the attenuated packing members.

In describing the operation of tower I it will be assumedthat the phase which is of greater density preferentially wets the packing members. If the opposite were true, it would be merely necessary to construct tower I40 up-side-down.

The liquid which preferentially wets the packing is fed onto rods 3I'a through metering tubes 39a thesameasinFigure 3.

This liquid flows along the attenuated packing members as it descends through tower I40, forms a layer at the bottom I 43 thereof and is withdrawn at I50.

If the liquid which is to form the substantial part of the other or second phase is to progress countercurrently of the first phase as in modes of operation (1), (4), and (5), this liquid enters the lowermost chamber I42 of tower I40 through a manifold I43, flows transversely of the tower and out of said chamber I42-through the other manifold I43.

' The latter manifold is connected to the next higher manifold. I43 preferably on the same side of the tower. The second phase ascends with or without the'aid of a pump and enters the next higher chamber I42 wherein it again flows transversely of the tower but preferably in a direction opposite from that in the first case, and leaves said next higher chamber I42 through the manifold I43 on the opposite side thereof.

Tower I 40. may be provided with any number of chambers I42 and if said number is even and the chambers I42 are connected serially in the manner described the second phase will flow laterally of the tower I40 the same number of times in both directions. This tends to prevent the first phase from concentrating on one side of the tower.

However, the second phase need not'necessarily flo'w transversely of tower I40 in opposite directions the same number of times and, in fact, may flow in one direction only should this be desired, or the manifolds may be so connected.

that the second phase is fed to each chamber I 42 at the same time and fiowstransversely of the .tbwer only'once, should this be desired. In the latter case the second' phase would progress neither countercurrently nor in the same direction as the first phase. In fact, the second phase may beheld stationary during'the contact in' which case the contact may be compared to that which takes place" in batch operations. Should it be desired to have the second phase progress in the same direction as the first phase chamber I42 or otherwise. would be specially connected to avoid locking ofas in mode of operation (6), it would be merely necessary to reverse the direction of flow of the second phase. The fiow might also alternate should this be desired for any reason. I

In mode of operation (2) the first phase might be comprised chiefly of oil and the second phase (or phases) chiefly of the two partially miscible or immiscible solvents. The solvent of greater density would be fed into the uppermost chamber I42 and the heavier final phase withdrawn from the lowermost chamber I42 or otherwise, and the solvent of lesser density would be fed into the lowermost chamber I42 and the lighter final phase withdrawn from the uppermost The manifolds I43 the two solvents against fiow. The oil might be fed into the towerthrough chamber 35a if its density is such. as to cause it to fiow. Otherwise, the oil may be introduced at an intermediate point. for instance, by employing a construction such as shown in Figure 5.

All of the oil might or might not be dissolved in the solvent. The two solvents might flow in layer form countercurrently or in the same direction through one chamber I42 only, if desired.

. continuous phase flow. They may, however, be

reversed..

Should the lateral flow of the second phase and/or the precipitation of materials from the second phase 'cause any substantial quantity of the first phase to become permanently separated from the attenuated packing members in any chamber I42, this separated portion .of the first 7 phase may be metered back onto rods 3Ia by providing apertures I44 with risers I52 and by arranging the upper edges I53 of the risers I52 of any plate I in a horizontal plane. Otherwise, the risers I52 may be omitted if desired.

Should the second phase preferentially wet the packing, it may be made to fiow either vertically or transversely of the tower, the first phase flowing in the other of the two directions.

The operation of tower I40 would be somewhat similar even though there were no well defined preferential wetting, care being taken to permit the desired separation of phases in chambers I42.

A plurality of anyof' the foregoing towers or a combination of such towers may be connected together in a manner so as to adapt 'such arrangement for a large number of the foregoing modes of operation.

Thisis illustrated in Figure 9 wherein towers I6I, I62, I63, and I64 are illustrated as being constructed similarly to tower I0.

Upper outlet I65 of tower I 6| is connected to lower inlet I66 of tower I62 through line I61 in which is shown a heat, exchanger I66 and a pump I68.

Upper outlet I" oftower I62 is connected to ,70

lower inlet I12 of tower I63 through. line I13 in which is shown a heat exchanger I14 and pump Upper outlet I11 of tower I 63 is connected to lower inlet I10 of tower I64 through line I10 in which is shown a heat exchanger I80 and pump Upper outletl88 may lead to a receiver or other point.

Lower outlet I 01 tower I84 is connected to' upper inlet I88, of tower I83 through line I81 in which is shown a pump I88 and heat exchanger 9 w ,A

Lower outlet I9I of tower I88 is connected to upper inlet I92 of tower I82 through line I93in which is shown a pump I94 and heat exchanger I95.

Lower outlet I91 01 tower I82 is connectedto upper inlet I98 of tower I8I through line I99 in which is shown a pump 200 and heat exchanger 20I.

Lower outlet 203 of tower I8I may lead to a receiver or other source.

Tower I84 is provided with an upper inlet 204 and tower I8I is provided with a lower inlet 205.

In mode of operation (1) the lighter phase' enters the system at 205, flows up through tower I8I, down through line I81, up through tower I82, down through line I13, up through tower I83, down through line I19, up through tower I84, and out of the system at- I83.

The heavier phase enters the system at 204, flows down through tower I84, up through line I81, down through tower I83, up through line I93, down through tower I82, up through line I99,

down through tower I8I, and out or the system- If desired side streams of the lighter phase might be taken off at 2I0, 2 and/or 2I2 and/or side streams of the heavier phase might be taken off at 201, 208 and/or 209.

In the mode of operation (411) the flow is the I same except that the solvent capacity of the solvent is reduced in the direction of solvent flow. For instance, if the solvent enters at 205, tower I8I may be operated at the highest temperature, tower I82 at the next highest temperature, tower I83 at the next highest temperature and tower I84 at the lowest temperature; or, the temperature "of the-lighter phase may be gradually reduced in succession by heat exchangers I88, I14, and I00; or both. The temperature might be reduced in any other manner, for instance, along the towers themselves.

. A precipitating solvent might be introduced into towers I84, I83, I82 and/or I8I at any desired point with or without the reduction of tem-' perature previously referred to.

Precipitation of oil might be effected by other means, for instance, by evaporation or other removal of solvent in place of or in addition to reduction in temperature and/or addition of another solvent.

If the solvent were introduced at 204 the temperature would,'of course, be progressively re duced in the opposite direction through the system from that just described.

If desired side streams of the lighter phase might be taken oil at 2I0, 2 and/or 2I2 and/ or side streams of the heavier phase might be taken off at 201, 208 and/or 209.

In mode of operation (41)) if the solvent were introduced into the system at 205, and the oil at I98, side streams of precipitated oil might be taken offat 201, 208 and/or 209.

If the oil were introduced at I92, side streams of precipitated oil might be taken off at 208 and/or 209 or,.if the oil were introduced at I88, a side stream of percipitated oil might be taken off at 209.

If the solvent were introduced into the system" at 204, the oil might enter the system ,at I18, I12 and/or I88 and side streams of precipitated oil might be taken of! at outlets 2I0, 2 and/or 2I2, depending upon the entry of oil.

Side streams or either phase, or course, might be taken or: at other points if desired.

It is to he noted, however, that no sidestream need be taken oil.-

It will be seen that modes of operation (40.) and (41)) might be combined.

In mode of operation (5) the solution may enter at 205 or at 204 depending upon the relative density of the" precipitate.

Assuming that the solution enters at 208, the first stage precipitate will be taken oil at 203.

The solution will enter column I82 at I88 either in the saturated condition in which it leaves column I8I or in an unsaturated condition by virtue of "the addition of heat, for instance, at heat exchanger I88 or of the addition of solvent, for instance, at I88.

The second stage precipitate will be taken of! at 201.

In a similar manner the solution flows through columns I83 and I84; and the third and fourth; stage precipitates are'taken off at 208 and 209 respectively.

' If only a part of the precipitate is withdrawn at each of 201, 208, and 209 we have the condition of a part of the precipitate in each stage except the very first, being fed back into the next preceding tower. The first stage precipitate may, of course, comprise merely scrubbed precipitate fed back from the second stage, in which case tower I8I would not be operated to directly cause other stage.

From the foregoing description the operation of the system when the solution enters at 204 will be obvious to persons skilled in the art.

In mode of operation (6) the two liquids merely progress through the system entering at 205 or at 204 depending upon'wh-ich phase is to travel the faster.

In mode of operation (2) one solvent enters at 205, the other at 204, and the oil may enter at I98, I88, I92, I12, I88, I18 and/or any other intermediate point or points.

In mode of operation (3) the oil may enter at 205 or at 204 depending upon its relative density with respect to the solvents, and the solvents may enter at any desired number of points along the flow of the oil.

The term solvent as used herein includes a mixture of solvents when used in place of a single It is, of course, understood that the temperature at some time during the treatment will be aoszs e ployed to form a single solution of all of the liquids.

It will also be understood that the contacting sections'of any of the towers described herein .may have any desired height. In choosing such height consideration will, of course, be given to the number of theoretically perfect batch contacts desired in the particular contacting section.

The efficiency of the packing will have its influence upon height since for the same results a more eflicient packing will require a lesser height than a less efficient packing.

. In one setup similar to that of Figure 1 having a contacting section equivalent to about forty feet with jack chain as packing in the tubes, between eight and twelve theoretically perfect batch contacts were obtained, depending upon the mode of operation adopted. The height per theoretically perfect batch contact might have been considerably reduced by substituting the small wire forms referred to above in place of jack chain.

It will be seen that a fundamental characteristic of similarity between the several modes of operation and towers described herein is found in the formation and maintenance .of a plurality of separate streams of at least one phase,this plurality of separate streams of one phase being brought into intimate contact with the other phase in a manner affording a high rate of lateral difiusion between the phases with a low rate of longitudinal diffusion in the individual phases,

Either phase may comprise any liquid or mixture of liquids whether in the solid, liquid, or

vapor phase at normal temperatures and pressures, the treatment of mineral oil and more particularly lubricating oil with solvents being set forth herein as a specific example.

A further fundamental characteristic of similarity resides in the solvent treatment of mineral oils and the various steps pertaining-thereto.

The various towers, modes of operation, and steps herein particularly described represent specific examples of applying the invention which is intended to be limited only as required by the prior art. Therefore, changes,'omissi0ns, additions, substitutions and/or modifications might be made without invention.

For convenience in description, the terms "vertically and uprightly as used in the specification and in the claims in describing the positioning of the attenuated packing members is intended to include not only a positioning wherein the packing members are perpendicular to the horizon but also a positioning wherein they are sufliciently so to function for the purposes set forth herein.

Also for convenience in description the term I rod as used in the specification and claims in describing the structure of certain attenuated packing members is used broadly and includes any other structure capable of a similar function whether it be solid or hollow, imperforate or perforate, unitary or articulated, or a connected series of links or rings such as jack chainor otherwise. a a

Reference is made to certain of applicants copending applications as follows: Serial No. 688,416 filed September 6, 1933, Serial No. 699,050 filed November 21, 1933, Serial No. 697,344 filed November 9, 1933, Serial No. 697,858 filed November 13, 1933, Serial No. 697,990 filed November 14,

departing from the spirit of the 1933 and Serial No. 735,026 filed July 13, 1934, which show several species and of one or more of which this application might be considered as a continuation in part.

We claim:

1. In a process for contacting liquid phases such as in the treatment of mineral ofls wherein oneliquid phase is caused to move through a zone of contact relative to another liquid phase by virtue of a difference in'density, the step of maintaining at least one phase in a widely distributed form by causing said relative movement between said phases to take place in the presence of a group of attenuated packing members arranged in the zone of contact side by side and longitudinally of the flow of at leastone phase-with each packing member of suflicient length to extend throughout at least a substantial portion of said zone of contact.

2. In a process for contacting liquid phases such as in the treatment of mineral oils wherein one liquid phase is caused to move through a zone of contact relative to another liquid phase by virtue of a difference in density, the step of maintaining phases to take place about a group of attenuated packing members arranged in the zone of contact side by side and longitudinally of the flow of said 1 phases with each packing member of suflic'ient length to extend throughout at least a substantial I portion of said zone of contact.

3. A process for the countercurrent contact of in a widely distributed form by causing a treating phase to move through a zone of contact countercurrently to a phase under treatment by virtue of a difference in density of said phases, said countercurrent movement between said phases taking place about a group of attenuated packing members arranged in the zone of contact side by side and longitudinally of the fiow of said phases withieach packingmember of suiiicient length to extend throughout at least a sub stantial portion of said zone of contact.

4. In a process for contacting liquid phases such as inthe treatment of mineral oils wherein one liquid phase is caused'to move through the zone of contact relative to another liquid phase by virtue of a difl'erence in density, the step of maintaining at least one phase in a widely dstributed form by causing said relative movement between said phases to take place about a group of individually unencased attenuated packing members arranged in the zone of contact side by side and longitudinally ofthe flow of at least one phase with each packing member of sufficient length to extend throughout at least a substantial portion of said zone of contact.

5. In a process for contacting liquid phases such as in the-solvent treatment of petroleum oil fractions, the. step of flowing said liquid phases relative to each other through a phase contacting zone in which at least one of said liquid phasesover a plurality of packing members each a which has a relatively long and generally narrow shape, sald'packing members being wetted by said liquid phase. a

7. In a process involving the counterflow of a mineral oiland a solvent by virtue of a diflerence in density for the purposes of contact, the steps of causing at least one of said liquids to flow through the common path of the counterflow in a widely distributed form by conducting said liquid through said common path in substantially equalamounts over a plurality of packing members each of which has a relatively long and generally narrow shape, said packing members being wetted by said liquid.

8. Inv a, process involving the counterflow of a mineral oil and a solvent by virtue of a difference in density for the purpose of contact, the steps of causing one of said liquids to flow through-the common path of the. counterflow in a substantially uniformly distributed fllm and drop form by conducting said liquid through said common path in substantially equal amounts over a plurality of elongated packing members at least for the most part of relatively small average crosssectional area, said packing members being wetted by said liquid, and shaping said packing members in a manner so that at least apart of said liquid will become detached in drops from said packing members and will recontact said packing members in the course of its flow.

9. In a process for contacting liquid phases such as in the solvent treatment of petroleum oil fractions, the step of countercurrently flowing said liquid phases through a phase contacting .zone in which each liquid phase is maintained throughout said phase contacting zone in a plurality of separate relatively small streams.

10. In a process for contacting'liquid phases such as in -the.solvent treatment of mineral oils, the steps of countercurrently flowing said liquid phases through a, phase contacting zone, maintaining ,each liquid phase while in said phase,

contacting zone in a plurality of separate relatively small streams, and contacting each stream of each liquid phase with a separate stream of another liquid phase in a segregated phase con- I tacting course in which each stream is caused to contact its associated stream over a relatively large area compared to its volume.

11. In a process involving the counterflow of a mineral oil and a solvent by virtue of a difference in density for the purposes of contact, the

steps of causing at least one of said liquids to flow through the common path of the counterflow in a widely distributed form by conducting said liquid through said common path in substantially equal amounts over a plurality of separate packing members arranged in relatively longand generally narrow shapes, said packing members being wetted by said liquid, and separately encasing each of said packing members to confine said counterflow to said packing members.

12. A process for counterflowing liquid phases by virtue of a diilerence in density for the purposes of contact such as in the solvent treatment of petroleum'oil fractions, comprising dividing 4 each liquid phase into a plurality of streams,

counterilowing said streams so that each stream of each liquid phase contacts one stream of each other liquid phase in an elongated phase contacting path which is segregated from all of the other streams, and substantially uniformly distributing the counterflowing streams acrm the cross section of each phase contacting path by confining the average cross section of each phase contacting path to a relatively small area.

13. In a process. for contacting liquid phases such as in the solvent treatment of mineral oils, the steps of countercurrently flowing said liquid phases through a phase contacting zone, maintaining each liquid phase while in said phase contacting zone in a plurality of separate relatively small streams, contacting each stream of each liquid phase with a separate stream of each other liquid phase in a segregated phase contacting coursein which each stream is caused to contact each associated-stream over a relatively large area compared to its volume, and maintaining the proportions of, said phases at least substantially identical in said segregated phase contacting courses.

14. A process for counterflowing a mineral oil and a solvent by virtue of a difference in density for the purposes of contact, comprising dividing each liquid into a plurality of streams of substantially equal size, counterflowing said streams so thateach stream of each liquid contacts one .stream of the other liquid in a path which is such as in the solvent treatment of mineral oil's, the steps of countercurrently flowing said liquid phases through a phase contacting zone, maintaining each liquid phase while in said phase contacting zone in a, plurality of separate relatively smallstreams, contactingeach stream of each liquid phase with a separate streamtof each other liquid phase in a segregated phase contacting course in which each stream is caused to'contact each associated stream over a relatively large area compared to its volume, maintaining the proportions of said phases at least substantially identical in said segregated phase contacting l courses; and maintaining said segregated phase contacting courses under at least substantially identical temperature conditions.

16. A process for contacting liquid phases such as in the solvent treatment of mineral oils wherein one liquid phase isa solvent for another liquid phase, comprising causing said phases to move countercurrently to'each other through a zone of contact by virtue of a difierence in density of said phases, maintaining at least one phase in a widely distributed form by causing said countercurrent movement between said phases to take place in the presence of a group of attenuated packing members arranged in the zone of contact side by side and longitudinally of the flow of said phases with each packing member of sumcient length to the phase under treatment is fed into the zone of contact at the end thereof.

18. A process as claimed in claim 16 wherein the phase under treatment is fed into the zone .of contact atan intermediate point, and wherein the zone of contact at least for the most part in a plurality of separate streams of substantially equal size, and precipitating and refluxing through the solution zone apart of the oil thus dissolved in said solvent.

20. In a process for treating a mineral oil with a solvent, the steps of countercurrently'flowing said oil and solvent through a phase contacting zone in which each liquid is maintained in a plurality of separate relatively small streams with each stream of one liquid contacting a separate stream of the other liquid in a segregated path, and precipitating a .part of the dissolved oil in said paths to set up reflux conditions in said paths.

21. In a process for treating a mineral oil with a solvent, the steps of countercurrently flowing said oil and solvent through a column in'which" each liquid is maintained in a plurality oi. relatively small streams with each stream of one liquid contacting a separate stream of the other liquid in a segregated path, feeding the solvent 'and oil phases into said paths at substantially the same ratio one to the other, precipitating in eachsegregated path a part of the dissolved oil,

and refluxing into the solution zone of each sag-- regated path the oil precipitated in said segregated path.

22. In a' process for precipitating a material such as mineral oil from solution in a selective solvent, the steps 01' causing the solvent and precipitate to flow countercurrently to each. other through a column while maintainingat least one of said liquids throughout the zone 01 contact at least for the most part in fllm form and in separate streams.

23. In a process for precipitating a material such as mineral oil from solution in a selective solvent, the steps of causing said solution and precipitate to flow countercurrently through a column while maintaining each liquid throughout the zone of contact in a plurality 01' separate.

streams, contacting each stream of each liquid with a. separate stream of the other liquid in a separate phase contacting path in said zone of contact, andmaintaining the proportion oi precipitate to solution at least substantially identical in each path.

24. In a process for precipitating less soluble components of a material such as mineral oil from a solution thereof in a selective solvent, the steps or flowing said solution through a column having a plurality oi phase contacting paths of relatively small cross sectional area, maintaining said solution in an unsaturated condition in a zone in each path, bringing said solution to a super-saturated condition in a zone in each path downstream of solvent flow from said first mentioned zone to cause precipitation in said path, flowing the precipitate in each path countercurrently to the solution passing therethrough and into the zone of solvent unsaturation in said path, and controlling the precipitation in each path so that the proportion of precipitate to solution will be at least substantially the same in each 'MERRELL R. FENSKE.

wmBERr B. McCLUER..-

' path. 

